JP2988508B2 - Method and apparatus for producing low-boiling hydrocarbon oil - Google Patents
Method and apparatus for producing low-boiling hydrocarbon oilInfo
- Publication number
- JP2988508B2 JP2988508B2 JP17934794A JP17934794A JP2988508B2 JP 2988508 B2 JP2988508 B2 JP 2988508B2 JP 17934794 A JP17934794 A JP 17934794A JP 17934794 A JP17934794 A JP 17934794A JP 2988508 B2 JP2988508 B2 JP 2988508B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- melt
- pyrolysis
- melting tank
- melting
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/62—Plastics recycling; Rubber recycling
Landscapes
- Processing Of Solid Wastes (AREA)
- Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、ポリ塩化ビニル（以
下、単に塩化ビニルともいう）を含むプラスチック廃棄
物から有用な低沸点炭化水素油を製造する低沸点炭化水
素油の製造方法および製造装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for producing a low-boiling hydrocarbon oil useful for producing useful low-boiling hydrocarbon oil from plastic waste containing polyvinyl chloride (hereinafter also referred to simply as "vinyl chloride"). About.
【０００２】[0002]
【従来の技術】従来の低沸点炭化水素油の製造方法とし
て、たとえば特開平３−８６７９１号公報に示されたも
のがある。2. Description of the Related Art As a conventional method for producing a low-boiling hydrocarbon oil, for example, there is one disclosed in Japanese Patent Application Laid-Open No. 3-86691.
【０００３】この製造方法においては、図２に示すよう
に、押出機１により軟化もしくは溶融状態として供給さ
れたプラスチックを溶融槽２内で十分溶融させて熱分解
槽３に移送し、熱分解槽３において、槽３内の溶融物の
一部を加熱炉４に循環させつつ約３５０℃〜４５０℃の
温度に加熱することにより溶融物を熱分解させる。次い
で、熱分解により生成した蒸気状生成物を分離器５に導
いて、蒸気状生成物中に存在する液粒径の比較的大きい
ミスト部分を分離し、残りの蒸気状生成物をゼオライト
触媒槽６に導入して接触転化させる。そして、接触転化
生成物を含む触媒槽６内の蒸気状生成物を冷却器７に導
いて冷却することにより、液化した低沸点炭化水素油と
ガス状物とを分離回収している。In this manufacturing method, as shown in FIG. 2, a plastic supplied in a softened or molten state by an extruder 1 is sufficiently melted in a melting tank 2 and transferred to a pyrolysis tank 3 where the plastic is supplied. In 3, a part of the melt in the tank 3 is heated to a temperature of about 350 ° C. to 450 ° C. while being circulated in the heating furnace 4 to thermally decompose the melt. Next, the vaporous product generated by the thermal decomposition is led to the separator 5 to separate a mist portion having a relatively large liquid particle size present in the vaporous product, and the remaining vaporous product is separated into a zeolite catalyst tank. 6 and catalytically converted. Then, the vaporized product in the catalyst tank 6 containing the catalytic conversion product is guided to the cooler 7 to be cooled, whereby the liquefied low-boiling hydrocarbon oil and the gaseous substance are separated and recovered.
【０００４】このとき、原料たるプラスチック中に塩化
ビニルが含まれていると、加熱時に塩化ビニルの脱塩酸
反応が起こって塩化水素ガスが発生するので、多量の塩
化ビニルを含プラスチックを原料とするときは塩化水素
ガス除去処理を行っている。たとえば、押出機１内で発
生して押出機１出口より流出する塩化水素ガスや溶融槽
２内で発生した塩化水素ガスは、大気とともにブロワー
吸引して湿式中和装置に導くことにより中和処理してい
る。また、熱分解槽３内で発生した塩化水素ガスは、槽
３内の蒸気状生成物をアルカリ性吸着剤を充填した乾式
中和装置内を通過させることにより中和処理している。At this time, if vinyl chloride is contained in the plastic as a raw material, a dehydrochlorination reaction of the vinyl chloride occurs during heating and hydrogen chloride gas is generated, so that a plastic containing a large amount of vinyl chloride is used as a raw material. Occasionally, a hydrogen chloride gas removal treatment is performed. For example, the hydrogen chloride gas generated in the extruder 1 and flowing out of the outlet of the extruder 1 and the hydrogen chloride gas generated in the melting tank 2 are blown together with the atmosphere by a blower and guided to a wet neutralization device to perform a neutralization treatment. doing. Further, the hydrogen chloride gas generated in the pyrolysis tank 3 is neutralized by passing the vaporous product in the tank 3 through a dry neutralization device filled with an alkaline adsorbent.
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、上記し
た従来の処理方法では、押出機１出口より流出する塩化
水素ガスが大気中の水分とともに凝縮して塩酸となり、
この塩酸によって押出機１出口付近が著しく腐食される
だけでなく、押出機１の内部でも、プラスチック中に含
まれている微量の水分が塩化水素ガスを吸収して塩酸と
なり、押出機１が著しく腐食されるという問題がある。However, in the above-mentioned conventional processing method, the hydrogen chloride gas flowing out of the extruder 1 is condensed with the moisture in the atmosphere to form hydrochloric acid,
This hydrochloric acid not only significantly corrodes the vicinity of the extruder 1 outlet, but also inside the extruder 1, a small amount of water contained in the plastic absorbs hydrogen chloride gas to form hydrochloric acid, and the extruder 1 is significantly repelled. There is a problem of corrosion.
【０００６】また、上記した脱塩酸反応の速度および量
はプラスチックの保持温度と滞留時間に支配されるが、
上記した従来の連続処理方式では、溶融槽内で十分に脱
塩酸反応を進めることは困難であり、そのため、熱分解
槽でも比較的多量の塩化水素ガスが発生することになっ
て、乾式中和装置に充填したアルカリ性吸着剤の寿命が
短かかったり、熱分解槽からの抜取残渣中のＴ−Ｃｌ量
が多いという問題がある。The rate and amount of the above-mentioned dehydrochlorination reaction are governed by the holding temperature and residence time of the plastic.
In the conventional continuous processing method described above, it is difficult to sufficiently promote the dehydrochlorination reaction in the melting tank, and therefore, a relatively large amount of hydrogen chloride gas is generated even in the thermal decomposition tank, so that dry neutralization is performed. There are problems that the life of the alkaline adsorbent filled in the apparatus is short and that the amount of T-Cl in the residue extracted from the pyrolysis tank is large.
【０００７】本発明は上記問題を解決するもので、溶融
槽における脱塩酸反応を促進して熱分解槽に移送される
Ｔ−Ｃｌ量を低減し、これにより、アルカリ性吸着剤の
寿命を長くし、かつ熱分解槽から系外へ排出される残渣
中のＴ−Ｃｌ量を低減するとともに、発生する塩化水素
ガスを好適に処理して周辺装置の腐食を防止することを
目的とするものである。The present invention solves the above-mentioned problems, and promotes the dehydrochlorination reaction in the melting tank to reduce the amount of T-Cl transferred to the pyrolysis tank, thereby extending the life of the alkaline adsorbent. Another object of the present invention is to reduce the amount of T-Cl in the residue discharged from the thermal decomposition tank to the outside of the system and to appropriately treat generated hydrogen chloride gas to prevent corrosion of peripheral devices. .
【０００８】[0008]
【課題を解決するための手段】上記問題を解決するため
に、本発明の低沸点炭化水素油の製造方法は、熱媒体を
加熱源とする溶融槽において原料プラスチックを溶融す
る溶融過程と、この溶融物を熱分解槽において熱分解し
て蒸気状生成物を生成させる熱分解過程と、溶融槽内の
溶融物を熱分解槽に導く供給系と熱分解槽内の溶融物を
溶融槽に還流する還流系とからなる移送過程とを含む低
沸点炭化水素油の製造方法であって、前記溶融過程にお
いて、溶融槽内に適当容量の溶融物を貯留するととも
に、熱媒体を加熱源として溶融物を脱塩酸反応を促進す
る適当温度に維持する状態で、原料プラスチックを常温
の状態で投入して、槽内の溶融物と攪拌混合しつつ溶融
させ、この溶融物を、前記供給系から分岐して溶融槽に
至る溶融槽循環系を通して溶融槽に循環させながら、原
料プラスチック中に含まれるポリ塩化ビニルの脱塩酸反
応がほぼ終了する適当時間にわたって、前記適当温度に
維持するとともに、槽内のガスを湿式中和装置に導いて
ガス中に合まれる前記脱塩酸反応により発生した塩化水
素ガスを中和処埋し、この溶融過程が行われる間に前記
熱分解過程において、溶融槽より予め導かれた溶融物
を、前記還流系から分岐して熱分解槽に至る熱分解槽循
環系を通して熱分解槽に循環させながら熱分解させ、前
記溶融過程が終了した後に、溶融槽内の溶融物を供給系
により熱分解槽に導くとともに、熱分解槽内の溶融物の
一部を還流系により溶融槽に還流させ、還流する溶融物
を溶融槽内の溶融物に対する希釈流体および加熱流体と
して作用させて、溶融槽内に適当容量の溶融物を貯留す
るものである。In order to solve the above problems, a method for producing a low-boiling hydrocarbon oil according to the present invention comprises a melting step of melting a raw plastic in a melting tank using a heat medium as a heating source, and a melting step. Pyrolysis process in which the melt is pyrolyzed in the pyrolysis tank to produce a vapor product, a supply system that guides the melt in the melting tank to the pyrolysis tank, and reflux of the melt in the pyrolysis tank to the melting tank A low boiling point hydrocarbon oil including a transfer process comprising a reflux system, wherein an appropriate volume of the melt is stored in a melting tank in the melting process.
The heat medium is used as a heat source to promote the dehydrochlorination reaction of the melt.
While maintaining the temperature at a suitable temperature, the raw material plastic is charged at room temperature, and is melted while being stirred and mixed with the melt in the tank.The melt is branched from the supply system and reaches the melting tank. while circulating the molten bath through the bath circulation system, over a reasonable time dehydrochlorination reaction of the polyvinyl chloride is almost finished contained in the raw material plastic, while maintaining the proper temperature, the gas in the tank to wet neutralizer The hydrogen chloride gas generated by the dehydrochlorination reaction introduced into the gas is neutralized and buried.During the thermal decomposition process, the molten material previously introduced from the melting tank is used during the melting process. Pyrolysis is performed while circulating the pyrolysis tank through a pyrolysis tank circulation system that branches from the reflux system to a pyrolysis tank, and after the melting process is completed, the melt in the melting tank is pyrolyzed by the supply system. Led to With a portion of the melt of the pyrolysis chamber is refluxed into the molten bath by recirculation system, and by the action of the melt to reflux as a diluting fluid and the heating fluid to melt the melting tank, suitable capacity molten bath To store the melt
It is those that.
【０００９】また、本発明の低沸点炭化水素油の製造方
法は、熱媒体を加熱源として原料プラスチックを溶融す
る溶融槽と、溶融槽よりも高い熱分解温度に維持され、
溶融槽で溶融した溶融物を熱分解して蒸気状生成物を生
成させる熱分解槽とを備えた低沸点炭化水素油の製造装
置において、原料プラスチックを常温の状態で溶融槽に
供給するスクリューフィーダと、前記熱媒体を加熱する
加熱手段と、溶融槽内の溶融物を熱分解槽に導く供給系
と、供給系から分岐して溶融槽に至り、溶融槽内の溶融
物を循環返送する溶融槽循環系と、熱分解槽内の溶融物
の一部を溶融槽に還流させる還流系と、還流系から分岐
して熱分解槽に至り、熱分解槽内の溶融物を循環返送す
る熱分解槽循環系と、溶融槽内の溶融物と原料プラスチ
ックとを攪拌混合する攪拌手段と、溶融槽内のガスを導
入して溶融槽内で発生した塩化水素ガスを中和処埋する
湿式中和装置と、熱分解槽内で生成した蒸気状生成物を
導入して蒸気状生成物中に含まれる塩化水素ガスを中和
処埋する乾式中和装置と、制御手段とを設け、この制御
手段により、前記溶融槽循環系と熱分解槽循環系とを適
宣調整して、溶融槽内の溶融物を、原料プラスチック中
に合まれるポリ塩化ビニルの脱塩酸反応がほば終了する
適当時間、溶融槽循環系を通して溶融槽に循環させつつ
槽内に保持するとともに、熱分解槽内の溶融物を熱分解
槽循環系を通して熱分解槽に循環させ、次いで、前記供
給系と還流系とを過宣調整して、前記適当時間保持した
溶融槽内の溶融物を供給系により熱分解槽に導くととも
に、熱分解槽内の溶融物の一部を還流系により溶融槽に
還流させて、溶融槽内に適当容量の溶融物を貯留し、か
つ前記加熱手段を適宣調整して溶融槽内の溶融物の温度
をポリ塩化ビニルの脱塩酸反応を促進する適当温度に保
持するように構成したものである。Further, in the method for producing a low-boiling hydrocarbon oil of the present invention, a melting tank for melting a raw material plastic using a heat medium as a heating source, and a pyrolysis temperature maintained higher than the melting tank,
A screw feeder for supplying a raw plastic to a melting tank at a normal temperature in a low-boiling hydrocarbon oil producing apparatus having a pyrolysis tank for thermally decomposing a melt melted in a melting tank to generate a vapor-like product. And a heating means for heating the heat medium, a supply system for guiding the melt in the melting tank to the pyrolysis tank, and a melt for branching from the supply system to the melting tank and circulating and returning the melt in the melting tank. A tank circulation system, a reflux system that refluxes part of the melt in the pyrolysis tank to the melting tank, and pyrolysis that branches off from the reflux system to the pyrolysis tank and circulates and returns the melt in the pyrolysis tank. A tank circulation system, a stirring means for stirring and mixing the molten material in the melting tank and the raw material plastic, and a wet neutralization for introducing a gas in the melting tank to neutralize and bury hydrogen chloride gas generated in the melting tank. Introduces the vaporous product generated in the pyrolysis tank A dry neutralization device for neutralizing and embedding hydrogen chloride gas contained in the product, and control means are provided, and the control means appropriately adjusts the circulation system of the melting tank and the circulation system of the pyrolysis tank, The molten material in the melting tank is circulated through the melting tank circulation system and held in the melting tank for an appropriate time when the dehydrochlorination reaction of polyvinyl chloride mixed with the raw material plastic is almost completed, and thermal decomposition is performed. The melt in the tank is circulated through the pyrolysis tank circulation system to the pyrolysis tank, and then the supply system and the reflux system are over-adjusted, and the melt in the melt tank held for the appropriate time is supplied by the supply system. In addition to the introduction to the pyrolysis tank, a part of the melt in the pyrolysis tank is returned to the melting tank by the reflux system , and an appropriate volume of the melt is stored in the melting tank.
The heating means is suitably adjusted to maintain the temperature of the melt in the melting tank at an appropriate temperature for promoting the dehydrochlorination reaction of polyvinyl chloride.
【００１０】[0010]
【作用】上記構成により、溶融槽内に常温の状態で供給
された原料プラスチックは、槽内に適当容量で貯留維持
された溶融物と攪拌混合され、溶融物により熱量の供給
と均一な熱伝導がなされる状態において溶融し、この溶
融物が槽内にて適当温度で適当時間保持される間に、原
料プラスチック中に含まれる塩化ビニルの脱塩酸反応が
ほぼ終了する。このとき、溶融槽内に貯留維持された溶
融物の少なくとも一部は熱分解槽内の溶融物が還流され
たものであるため、槽内の溶融物は、還流された溶融物
により希釈されて適当粘度となるとともに還流する溶融
物から熱量の供給を受けており、これにより、原料プラ
スチックの溶融が促進される。脱塩酸反応により発生し
た溶融槽内の塩化水素ガスは、湿式中和装置において中
和処理される。この工程がバッチ式で行われるので、脱
塩酸反応が不十分な塩化ビニルを含まない、Ｔ−Ｃｌ量
の低減された溶融物が熱分解槽に移送される。According to the above construction, the raw material plastic supplied at room temperature into the melting tank is stirred and mixed with the melt stored and maintained in an appropriate volume in the tank, and the supply of heat and uniform heat conduction by the melt. While the melt is kept in a bath at an appropriate temperature for an appropriate time, the dehydrochlorination reaction of vinyl chloride contained in the raw material plastic is almost completed. At this time, at least a part of the molten material stored and maintained in the melting tank is the melt in the pyrolysis tank refluxed, so the melt in the tank is diluted by the refluxed melt. Heat is supplied from the melt which has an appropriate viscosity and is refluxed, and thereby the melting of the raw material plastic is promoted. The hydrogen chloride gas in the melting tank generated by the dehydrochlorination reaction is neutralized in a wet neutralizer. Since this step is carried out in a batch system, a molten material having a reduced amount of T-Cl, which does not contain vinyl chloride having an insufficient dehydrochlorination reaction, is transferred to the pyrolysis tank.
【００１１】そして、このような溶融物が熱分解槽にお
いて熱分解され、熱分解により生成した蒸気状生成物が
乾式中和装置に導かれるが、溶融槽において溶融物中の
Ｔ−Ｃｌ量が予め低減されているので、熱分解槽で生成
する塩化水素ガス量は少なく、この結果、乾式中和装置
に充填されるアルカリ性吸着剤の寿命が長くなるととも
に、熱分解槽から系外へ排出される残渣中のＴ−Ｃｌ量
や、最終生成物たる低沸点炭化水素油中のＴ−Ｃｌ量も
低減される。[0011] Then, such a melt is pyrolyzed in a pyrolysis tank, and a vapor-like product generated by the pyrolysis is led to a dry neutralization device, where the amount of T-Cl in the melt is reduced. Since it has been reduced in advance, the amount of hydrogen chloride gas generated in the pyrolysis tank is small, and as a result, the life of the alkaline adsorbent filled in the dry neutralization device is prolonged, and the alkaline adsorbent is discharged out of the system from the pyrolysis tank. The amount of T-Cl in the residue and the amount of T-Cl in the low-boiling hydrocarbon oil as the final product are also reduced.
【００１２】[0012]
【実施例】以下、本発明の実施例を図面を参照しながら
説明する。図１に示すように、低沸点炭化水素油の製造
装置は、プラスチックＰを溶融させる溶融槽１１と、溶
融槽１１で溶融された溶融物を熱分解させる熱分解槽１
２と、熱分解槽１２で発生した蒸気状生成物を接触転化
させるゼライトなどの触媒を充填した触媒槽１３と、触
媒槽１３内の蒸気状生成物を導入し、冷却して低沸点炭
化水素油を液化させる冷却器１４とを備えている。な
お、プラスチックＰは、ポリ塩化ビニル（ＰＶＣ）を多
量に含むポリオレフィン系のプラスチック（ＰＥ、Ｐ
Ｐ）およびＰＳなどであり、乾燥粉砕して投入される。Embodiments of the present invention will be described below with reference to the drawings. As shown in FIG. 1, an apparatus for producing a low-boiling hydrocarbon oil includes a melting tank 11 for melting a plastic P and a pyrolysis tank 1 for thermally decomposing a molten material in the melting tank 11.
2, a catalyst tank 13 filled with a catalyst such as zeolite for catalytically converting the vaporous product generated in the pyrolysis tank 12, and the vaporous product in the catalyst tank 13 are introduced, cooled and cooled to a low boiling point hydrocarbon. And a cooler 14 for liquefying the oil. The plastic P is a polyolefin-based plastic (PE, P) containing a large amount of polyvinyl chloride (PVC).
P) and PS, etc., which are supplied after being dried and pulverized.
【００１３】溶融槽１１の上方には、プラスチックＰを
投入するホッパ１５と、ホッパ１５から落とし込まれた
プラスチックＰを常温の状態で送り出すスクリューフィ
ーダ１６などの原料供給機とが設けられている。Above the melting tank 11, there are provided a hopper 15 for charging the plastic P and a material feeder such as a screw feeder 16 for feeding the plastic P dropped from the hopper 15 at a normal temperature.
【００１４】溶融槽１１は、下部寄りの外周部が熱媒体
循環部１７で覆われ、この熱媒体循環部１７に導かれる
熱媒油からなる熱媒体は、熱媒体加熱炉１８の加熱経路
１８ａに接続する循環経路１９を循環ポンプ２０の駆動
により循環される。そして、熱媒体加熱炉１８の加熱経
路１８ａで加熱された熱媒体が溶融槽１１の熱媒体循環
部１７に循環されて、溶融槽１１内の溶融物とプラスチ
ックＰとの混合物を加熱する。溶融槽１１の内部には、
槽内の混合物を攪拌混合する攪拌機２１が槽外のモータ
２２に接続して設けられている。溶融槽１１の上部に設
けられたベント管２３は、ポンプ２４ａを備えた湿式中
和装置２４に接続している。The melting tank 11 has an outer peripheral portion closer to the lower portion covered with a heating medium circulating section 17, and a heating medium made of a heating medium oil guided to the heating medium circulating section 17 is supplied to a heating path 18 a of a heating medium heating furnace 18. Is circulated by driving a circulation pump 20. Then, the heat medium heated in the heating path 18 a of the heat medium heating furnace 18 is circulated to the heat medium circulating section 17 of the melting tank 11 to heat the mixture of the melt and the plastic P in the melting tank 11. Inside the melting tank 11,
A stirrer 21 for stirring and mixing the mixture in the tank is provided connected to a motor 22 outside the tank. The vent pipe 23 provided at the upper part of the melting tank 11 is connected to a wet neutralizer 24 having a pump 24a.
【００１５】また、溶融槽１１の底部に接続して、溶融
槽１１内の溶融物を移送する供給ポンプ２５を介装した
供給経路２６が設けられており、供給経路２６が分岐し
た一方の分岐管２６ａは溶融槽１１に接続し、他方の分
岐管２６ｂは熱分解槽１２に接続している。また、熱分
解槽１２の下部に接続して、熱分解槽１２内の溶融物の
一部を還流する還流ポンプ２７を介装した還流経路２８
が設けられており、還流経路２８が分岐した一方の分岐
管２８ａは溶融槽１１に接続し、他方の分岐管２８ｂは
熱分解槽１２に接続している。分岐管２６ａ，２６ｂ，
２８ａ，２８ｂはそれぞれ、電動弁２６ｃ，２６ｄ，２
８ｃ，２８ｄを備えている。A supply path 26 connected to the bottom of the melting tank 11 and provided with a supply pump 25 for transferring the melt in the melting tank 11 is provided. The pipe 26a is connected to the melting tank 11, and the other branch pipe 26b is connected to the pyrolysis tank 12. A reflux path 28 connected to a lower portion of the pyrolysis tank 12 and having a reflux pump 27 interposed therein for refluxing a part of the melt in the pyrolysis tank 12.
Is provided, and one branch pipe 28a from which the reflux path 28 branches is connected to the melting tank 11, and the other branch pipe 28b is connected to the thermal decomposition tank 12. The branch pipes 26a, 26b,
28a, 28b are motorized valves 26c, 26d, 2 respectively.
8c and 28d.
【００１６】さらに、溶融槽１１は、槽内の溶融物の温
度および容量を検出する検出手段２９を設け、この検出
手段２９を検出ライン３０により制御装置３１に接続さ
せている。制御装置３１は、制御ライン３１ａにより熱
媒体加熱炉１８の加熱手段１８ｂに接続していて、加熱
手段１８ｂを通して加熱経路１８ａを制御することによ
り溶融槽１１の壁温を３００〜３４０℃として槽内の混
合物の温度をプラスチックの熱分解温度より低い、塩化
ビニルの脱塩酸反応に適当な３２０℃未満の温度に保持
する。また、制御装置３１は、制御ライン３１ｂ，３１
ｃ，３１ｄ，３１ｅ，３１ｆ，３１ｇにより供給ポンプ
２５、還流ポンプ２７、電動弁２６ｃ，２６ｄ，２８
ｃ，２８ｄに接続していて、溶融槽１１内に溶融物を常
時貯留維持するよう制御するとともに、溶融槽１１内の
溶融物の移送と、熱分解槽１２内の溶融物の還流を制御
する。Further, the melting tank 11 is provided with a detecting means 29 for detecting the temperature and the volume of the melt in the tank, and this detecting means 29 is connected to a control device 31 via a detecting line 30. The control device 31 is connected to the heating means 18b of the heating medium heating furnace 18 through a control line 31a, and controls the heating path 18a through the heating means 18b to set the wall temperature of the melting tank 11 to 300 to 340 ° C. The mixture is kept at a temperature below the pyrolysis temperature of the plastic, below 320 ° C., which is suitable for the dehydrochlorination of vinyl chloride. Further, the control device 31 includes control lines 31b, 31
The supply pump 25, the recirculation pump 27, and the motor-operated valves 26c, 26d, 28 are controlled by c, 31d, 31e, 31f, 31g.
c, 28d to control the melt to be constantly stored and maintained in the melt tank 11, and to control the transfer of the melt in the melt tank 11 and the reflux of the melt in the pyrolysis tank 12. .
【００１７】熱分解槽１２は、循環ポンプ３２を備えた
循環経路３３を介して溶融プラスチック加熱炉３４の加
熱経路３４ａに接続しており、熱分解槽１２内の溶融物
を加熱経路３４ａにおいて約３５０℃〜４５０℃の熱分
解温度まで加熱する。熱分解槽１２の上部のガス出口に
は凝縮器３５が接続されていて、熱分解槽１２より流入
した蒸気状生成物のうち液粒径の比較的大きいミスト部
分を分離して還流経路３６により熱分解槽１２に還流す
るようになっている。The pyrolysis tank 12 is connected to a heating path 34a of a molten plastic heating furnace 34 through a circulation path 33 provided with a circulation pump 32, and the molten material in the pyrolysis tank 12 is passed through the heating path 34a. Heat to a pyrolysis temperature of 350 ° C to 450 ° C. A condenser 35 is connected to a gas outlet at the upper part of the pyrolysis tank 12, and a mist portion having a relatively large liquid particle size is separated from a vapor-like product flowing from the pyrolysis tank 12 by a reflux path 36. The heat is returned to the thermal decomposition tank 12.
【００１８】凝縮器３５の下流には、アルカリ性吸着剤
を充填した乾式中和装置３７，３８が弁３７ａ，３７
ｂ，３８ａ，３８ｂにより切換え自在に設けられてい
て、凝縮器３５を通過した蒸気状生成物を導入して蒸気
状生成物中に含まれる塩化水素ガスを中和処理するよう
になっている。Downstream of the condenser 35, dry neutralizers 37, 38 filled with an alkaline adsorbent are provided with valves 37a, 37.
b, 38a, and 38b are provided so as to be freely switchable, so that a vapor-like product that has passed through the condenser 35 is introduced to neutralize the hydrogen chloride gas contained in the vapor-like product.
【００１９】触媒槽１３は乾式中和装置３７，３８の下
流に設けられ、冷却器１４は触媒槽１３の下流に設けら
れている。冷却器１４の先端には、冷却器１４からの流
出物を導入する気液分離槽３９が設けられている。４
０，４１は残渣取出装置である。The catalyst tank 13 is provided downstream of the dry neutralizers 37 and 38, and the cooler 14 is provided downstream of the catalyst tank 13. At the tip of the cooler 14, a gas-liquid separation tank 39 for introducing the effluent from the cooler 14 is provided. 4
Numerals 0 and 41 are residue removing devices.
【００２０】以下、上記構成における作用を説明する。
溶融槽１１内に熱分解槽１２より還流された溶融物を含
む適当量の溶融物を貯留維持し、電動弁２６ｃを開放す
るとともに電動弁２６ｄを閉じ、供給ポンプ２５を駆動
して、槽１１内の溶融物を供給経路２６、分岐管２６ａ
を経て溶融槽１１に戻る経路で循環させる。また、熱分
解槽１２内に溶融槽１１より移送された溶融物を貯留
し、電動弁２８ｃを閉じるとともに電動弁２８ｄを開放
し、還流ポンプ２７を駆動して、槽１２内の溶融物を還
流経路２８、分岐管２８ｂを経て熱分解槽１２に戻る経
路で循環させる。The operation of the above configuration will be described below.
An appropriate amount of molten material including the molten material refluxed from the pyrolysis tank 12 is stored and maintained in the melting tank 11, the electric valve 26c is opened, the electric valve 26d is closed, and the supply pump 25 is driven to drive the tank 11 The melt in the supply path 26, the branch pipe 26a
And circulates in a path returning to the melting tank 11. Further, the melt transferred from the melting tank 11 is stored in the pyrolysis tank 12, the electric valve 28 c is closed and the electric valve 28 d is opened, and the reflux pump 27 is driven to return the melt in the tank 12. Circulation is performed in a path returning to the pyrolysis tank 12 through the path 28 and the branch pipe 28b.
【００２１】この状態において、ホッパ１５に投入され
たプラスチックＰをスクリューフィーダ１６により常温
の状態で溶融槽１１に供給し、槽１１内の溶融物と攪拌
機２１により攪拌混合しながら熱媒体循環部１７により
維持される約３００℃の適当温度で適当時間保持する。
するとこの間に、プラスチックＰは、槽１１内の溶融物
により熱量の供給と均一な熱伝導がなされる状態におい
て十分溶融し、プラスチックＰ中に含まれる塩化ビニル
は脱塩酸反応を起こして塩化水素ガスを放出する。槽１
１内のガスはベント管２３を通じて湿式中和装置２４に
導かれ、ガス中に含まれる塩化水素ガスは水に溶解して
塩酸となった後にポンプ２４ａにより取り出されて中和
処理される。このように、槽１１内に適当時間保持する
バッチ式にて処理されることにより、塩化ビニルの脱塩
酸反応はほぼ完全に終了し、溶融物中のＴ−Ｃｌ量は低
減される。In this state, the plastic P charged into the hopper 15 is supplied to the melting tank 11 at a normal temperature by the screw feeder 16 and is mixed with the molten material in the tank 11 by the stirrer 21 while stirring and mixing with the heat medium circulating section 17. At a suitable temperature of about 300 ° C. maintained for a suitable time.
Then, during this time, the plastic P is sufficiently melted in a state in which heat is supplied and uniform heat conduction is performed by the molten material in the tank 11, and vinyl chloride contained in the plastic P undergoes a dehydrochlorination reaction to generate hydrogen chloride gas. Release. Tank 1
The gas in 1 is led to a wet neutralization device 24 through a vent pipe 23, and the hydrogen chloride gas contained in the gas is dissolved in water to form hydrochloric acid, and then taken out by a pump 24a for neutralization. In this way, by performing the treatment in a batch manner in which the mixture is held in the tank 11 for an appropriate time, the dehydrochlorination reaction of vinyl chloride is almost completely completed, and the amount of T-Cl in the melt is reduced.
【００２２】このとき、熱分解槽１２においては、槽１
２内の溶融物の一部が加熱炉３４に循環される状態で溶
融物が熱分解温度に加熱されて熱分解される。なお、熱
分解槽１２内の溶融物は、溶融槽１１における前バッチ
の溶融物が移送されたものである。熱分解槽１２内で生
成した蒸気状生成物は、凝縮器３５において液粒径の比
較的大きいミスト部分が分離された後に乾式中和装置３
７，３８のいずれかに導かれ、乾式中和装置３７，３８
に充填されたアルカリ性吸着剤により塩化水素ガスが中
和処理される。そして、残りの蒸気状生成物が触媒槽１
３に導入されて接触転化される。接触転化された生成物
を含む触媒槽１３内の蒸気状生成物は冷却器１４に導か
れて冷却された後に気液分離槽３９に流入し、ガス状物
４２は気液分離槽３９の外部へ導かれ、冷却器１４で液
化した低沸点炭化水素油４３は気液分離槽３９内に貯留
される。このとき、溶融槽１１より移送された溶融物中
のＴ−Ｃｌ量が低減されているので、熱分解槽１２内で
生成する塩化水素ガス量は少なく、乾式中和装置３７，
３８に充填されるアルカリ性吸着剤の寿命が長くなると
ともに、熱分解槽１２から残渣取出装置４１を通じて系
外へ排出される残渣中のＴ−Ｃｌ量や、最終生成物たる
低沸点炭化水素油４３中のＴ−Ｃｌ量が低減される。At this time, in the thermal decomposition tank 12, the tank 1
While a part of the melt in 2 is circulated to the heating furnace 34, the melt is heated to a pyrolysis temperature and pyrolyzed. The melt in the pyrolysis tank 12 is the one from which the melt of the previous batch in the melt tank 11 was transferred. The vapor-like product generated in the pyrolysis tank 12 is separated from the mist portion having a relatively large liquid particle size in the condenser 35 after the dry neutralization device 3.
7 and 38, and the dry neutralizers 37 and 38
The hydrogen chloride gas is neutralized by the alkaline adsorbent filled in the container. Then, the remaining vaporous product is transferred to the catalyst tank 1
3 and catalytically converted. The vapor-like product in the catalyst tank 13 containing the catalytically converted product flows into the gas-liquid separation tank 39 after being guided and cooled by the cooler 14, and the gaseous substance 42 flows outside the gas-liquid separation tank 39. The low-boiling hydrocarbon oil 43 liquefied by the cooler 14 is stored in the gas-liquid separation tank 39. At this time, since the amount of T-Cl in the melt transferred from the melting tank 11 is reduced, the amount of hydrogen chloride gas generated in the pyrolysis tank 12 is small, and the dry neutralizer 37,
As the life of the alkaline adsorbent filled in the fuel tank 38 becomes longer, the amount of T-Cl in the residue discharged from the pyrolysis tank 12 to the outside of the system through the residue removal device 41 and the low-boiling hydrocarbon oil 43 as the final product The amount of T-Cl therein is reduced.
【００２３】このようにして、装置全体の運転を中止す
ることなく、溶融槽１１における溶融処理および熱分解
槽１２における熱分解処理を独立して行い、溶融槽１１
における脱塩酸反応がほぼ終了したら、制御装置３１に
よって、電動弁２６ｄを開放するとともに電動弁２６ｃ
を閉じ、供給ポンプ２５にて、溶融槽１１内の溶融物を
供給経路２６、分岐管２６ｂを経て熱分解槽１２に移送
する。また、電動弁２８ｃを開放するとともに電動弁２
８ｄを閉じ、還流ポンプ２７にて、熱分解槽１２内の溶
融物の一部を還流経路２８、分岐管２８ａを経て溶融槽
１１に還流させる。その後、上記と同様にして、溶融槽
１１における溶融処理および熱分解槽１２における熱分
解処理を独立して行う。このとき、溶融槽１１内の溶融
物は、熱分解槽１２より還流された溶融物によって粘度
低下されるとともに熱量供給されているので、均一な熱
伝導が可能となる。In this way, the melting process in the melting tank 11 and the pyrolysis process in the pyrolysis tank 12 are performed independently without stopping the operation of the entire apparatus.
When the dehydrochlorination reaction in is substantially completed, the controller 31 opens the motor-operated valve 26d and the motor-operated valve 26c
Is closed, and the supply pump 25 transfers the melt in the melting tank 11 to the thermal decomposition tank 12 via the supply path 26 and the branch pipe 26b. Further, the electric valve 28c is opened and the electric valve 2 is opened.
8d is closed, and a part of the melt in the pyrolysis tank 12 is returned to the melting tank 11 via the return path 28 and the branch pipe 28a by the reflux pump 27. Then, similarly to the above, the melting process in the melting tank 11 and the pyrolysis process in the pyrolysis tank 12 are independently performed. At this time, since the melt in the melting tank 11 is reduced in viscosity by the melt refluxed from the thermal decomposition tank 12 and supplied with heat, uniform heat conduction becomes possible.
【００２４】なお、電動弁２６ｃ，２６ｄ，２８ｃ，２
８ｄの切換を行う時間を適宜調節することにより、投入
される塩化ビニルの特性に応じた適切な溶融槽内保持時
間を確保できる。塩化ビニルを含まないプラスチックを
処理する場合は、従来の連続処理方式を行うことができ
る。The motor-operated valves 26c, 26d, 28c, 2
By appropriately adjusting the switching time of 8d, it is possible to secure an appropriate holding time in the melting tank according to the characteristics of the vinyl chloride to be charged. When processing plastics containing no vinyl chloride, a conventional continuous processing method can be used.
【００２５】また、溶融槽１１においてプラスチックＰ
を十分溶融できるので、スクリューフィーダー１６によ
り常温の状態で供給すればよく、従来のような押出機を
用いる必要がないため設備費を低減できる。発生した塩
化水素ガスは中和装置において好適に処理されるので、
装置の腐食は軽減され、設備寿命は長くなる。In the melting tank 11, the plastic P
Can be sufficiently melted and supplied at room temperature by the screw feeder 16, and the equipment cost can be reduced because it is not necessary to use an extruder as in the related art. Since the generated hydrogen chloride gas is suitably processed in the neutralization device,
Equipment corrosion is reduced and equipment life is extended.
【００２６】[0026]
【発明の効果】以上のように、本発明によれば、原料プ
ラスチックを常温の状態で溶融槽に供給して溶融させ、
この溶融物を適当温度で適当時間槽内に保持して、原料
プラスチック中に含まれる塩化ビニルの脱塩酸反応を溶
融槽においてほぼ終了させ、脱塩酸反応により発生した
塩化水素ガスは湿式中和装置において中和処理するよう
にした。この結果、Ｔ−Ｃｌ量の低減された溶融物が熱
分解槽に移送されて熱分解されることになり、熱分解槽
で生成する塩化水素ガス量が少なくなって、乾式中和装
置に充填されるアルカリ性吸着剤の寿命が長くなるとと
もに、熱分解槽から系外へ排出される残渣中のＴ−Ｃｌ
量や、最終生成物たる低沸点炭化水素油中のＴ−Ｃｌ量
が低減され、低沸点炭化水素油の付加価値が向上する。As described above, according to the present invention, the raw plastic is supplied to the melting tank at normal temperature and melted.
This molten material is held in a tank at an appropriate temperature for an appropriate time, and the dehydrochlorination reaction of vinyl chloride contained in the raw material plastic is almost completed in the melting tank, and the hydrogen chloride gas generated by the dehydrochlorination reaction is wet-neutralized. And neutralized. As a result, the melt having a reduced amount of T-Cl is transferred to the pyrolysis tank and pyrolyzed, and the amount of hydrogen chloride gas generated in the pyrolysis tank is reduced, so that the dry neutralizer is filled. The life of the alkaline adsorbent is extended, and the T-Cl in the residue discharged from the pyrolysis tank to the outside of the system is increased.
The amount and the amount of T-Cl in the low-boiling hydrocarbon oil as the final product are reduced, and the added value of the low-boiling hydrocarbon oil is improved.
【００２７】また、溶融槽において原料プラスチックを
十分溶融できるので、従来のような押出機を用いる必要
がなくなり、設備費を低減できる。さらに、発生した塩
化水素ガスは中和装置において好適に処理されるので、
装置の腐食が軽減され、設備寿命が長くなる。Further, since the raw material plastic can be sufficiently melted in the melting tank, it is not necessary to use an extruder as in the prior art, and the equipment cost can be reduced. Further, since the generated hydrogen chloride gas is suitably processed in the neutralization device,
Equipment corrosion is reduced and equipment life is extended.
【図１】本発明の一実施例の低沸点炭化水素油の製造装
置の全体構成を示した説明図である。FIG. 1 is an explanatory diagram showing an overall configuration of a low-boiling hydrocarbon oil producing apparatus according to one embodiment of the present invention.
【図２】従来の低沸点炭化水素油の製造装置の全体構成
を示した説明図である。FIG. 2 is an explanatory diagram showing the overall configuration of a conventional low-boiling hydrocarbon oil producing apparatus.
Ｐ 原料プラスチック 11 溶融槽 12 熱分解槽 16 スクリューフィーダ 18 熱媒体加熱炉 21 攪拌機 24 湿式中和装置 25 供給ポンプ 26 供給経路 26a 分岐管（溶融槽循環系） 27 還流ポンプ 28 還流経路 28b 分岐管（熱分解槽循環系） 31 制御装置 37,38 乾式中和装置 P Raw material plastic 11 Melting tank 12 Pyrolysis tank 16 Screw feeder 18 Heat medium heating furnace 21 Stirrer 24 Wet neutralizer 25 Supply pump 26 Supply path 26a Branch pipe (melting tank circulation system) 27 Reflux pump 28 Return path 28b Branch pipe ( Pyrolysis tank circulation system) 31 Controller 37,38 Dry neutralizer
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平７−102264（ＪＰ，Ａ) 特開 平６−65582（ＪＰ，Ａ) (58)調査した分野(Int.Cl.6，ＤＢ名) C10G 1/10 B09B 3/00 ────────────────────────────────────────────────── ─── Continuation of the front page (56) References JP-A-7-102264 (JP, A) JP-A-6-65582 (JP, A) (58) Fields investigated (Int. Cl. 6 , DB name) C10G 1/10 B09B 3/00
Claims (2)
料プラスチックを溶融する溶融過程と、この溶融物を熱
分解槽において熱分解して蒸気状生成物を生成させる熱
分解過程と、溶融槽内の溶融物を熱分解槽に導く供給系
と熱分解槽内の溶融物を溶融槽に還流する還流系とから
なる移送過程とを含む低沸点炭化水素油の製造方法であ
って、 前記溶融過程において、溶融槽内に適当容量の溶融物を
貯留するとともに、熱媒体を加熱源として溶融物を脱塩
酸反応を促進する適当温度に維持する状態で、原料プラ
スチックを常温の状態で投入して、槽内の溶融物と攪拌
混合しつつ溶融させ、この溶融物を、前記供給系から分
岐して溶融槽に至る溶融槽循環系を通して溶融槽に循環
させながら、原料プラスチック中に含まれるポリ塩化ビ
ニルの脱塩酸反応がほぼ終了する適当時間にわたって、
前記適当温度に維持するとともに、槽内のガスを湿式中
和装置に導いてガス中に合まれる前記脱塩酸反応により
発生した塩化水素ガスを中和処埋し、 この溶融過程が行われる間に前記熱分解過程において、
溶融槽より予め導かれた溶融物を、前記還流系から分岐
して熱分解槽に至る熱分解槽循環系を通して熱分解槽に
循環させながら熱分解させ、 前記溶融過程が終了した後に、溶融槽内の溶融物を供給
系により熱分解槽に導くとともに、熱分解槽内の溶融物
の一部を還流系により溶融槽に還流させ、還流する溶融
物を溶融槽内の溶融物に対する希釈流体および加熱流体
として作用させて、溶融槽内に適当容量の溶融物を貯留
することを特徴とする低沸点炭化水素油の製造方法。1. A melting process in which a raw material plastic is melted in a melting tank using a heat medium as a heating source, a pyrolysis process in which the melt is pyrolyzed in a pyrolysis tank to generate a vapor-like product, and a melting tank. A method for producing a low-boiling hydrocarbon oil, comprising: a transfer system comprising a supply system for introducing the melt in the pyrolysis tank to the pyrolysis tank and a reflux system for refluxing the melt in the pyrolysis tank to the melting tank. In the process, an appropriate volume of molten material is placed in the melting tank.
Storing and desalting the melt using a heat medium as a heating source
While maintaining the appropriate temperature for accelerating the acid reaction, the raw material plastic is charged at room temperature and melted while stirring and mixing with the melt in the tank.The melt is branched from the supply system and melted. While circulating in the melting tank through the melting tank circulation system leading to the tank, over a suitable time when the dehydrochlorination reaction of polyvinyl chloride contained in the raw plastic is almost completed
While maintaining the appropriate temperature, the gas in the tank is guided to a wet neutralization device to neutralize and embed the hydrogen chloride gas generated by the dehydrochlorination reaction mixed in the gas. In the pyrolysis process,
The molten material previously guided from the melting tank is pyrolyzed while being circulated to the pyrolysis tank through a pyrolysis tank circulation system that branches from the reflux system and reaches the pyrolysis tank. While the melt inside is guided to the pyrolysis tank by the supply system, a part of the melt in the pyrolysis tank is returned to the melting tank by the reflux system, and the returning melt is diluted with the dilution fluid for the melt in the melting tank. Acts as a heating fluid and stores an appropriate volume of molten material in the melting tank
A method for producing a low-boiling hydrocarbon oil.
を溶融する溶融槽と、溶融槽よりも高い熱分解温度に維
持され、溶融槽で溶融した溶融物を熱分解して蒸気状生
成物を生成させる熱分解槽とを備えた低沸点炭化水素油
の製造装置において、 原料プラスチックを常温の状態で溶融槽に供給するスク
リューフィーダと、前記熱媒体を加熱する加熱手段と、
溶融槽内の溶融物を熱分解槽に導く供給系と、供給系か
ら分岐して溶融槽に至り、溶融槽内の溶融物を循環返送
する溶融槽循環系と、熱分解槽内の溶融物の一部を溶融
槽に還流させる還流系と、還流系から分岐して熱分解槽
に至り、熱分解槽内の溶融物を循環返送する熱分解槽循
環系と、溶融槽内の溶融物と原料プラスチックとを攪拌
混合する攪拌手段と、溶融槽内のガスを導入して溶融槽
内で発生した塩化水素ガスを中和処埋する湿式中和装置
と、熱分解槽内で生成した蒸気状生成物を導入して蒸気
状生成物中に含まれる塩化水素ガスを中和処埋する乾式
中和装置と、制御手段とを設け、 この制御手段により、前記溶融槽循環系と熱分解槽循環
系とを適宣調整して、溶融槽内の溶融物を、原料プラス
チック中に合まれるポリ塩化ビニルの脱塩酸反応がほば
終了する適当時間、溶融槽循環系を通して溶融槽に循環
させつつ槽内に保持するとともに、熱分解槽内の溶融物
を熱分解槽循環系を通して熱分解槽に循環させ、次い
で、前記供給系と還流系とを過宣調整して、前記適当時
間保持した溶融槽内の溶融物を供給系により熱分解槽に
導くとともに、熱分解槽内の溶融物の一部を還流系によ
り溶融槽に還流させて、溶融槽内に適当容量の溶融物を
貯留し、かつ前記加熱手段を適宣調整して溶融槽内の溶
融物の温度をポリ塩化ビニルの脱塩酸反応を促進する適
当温度に保持するよう構成したことを特徴とする低沸点
炭化水素油の製造装置。2. A melting tank for melting the raw material plastic using a heat medium as a heating source, and a pyrolysis temperature maintained at a higher pyrolysis temperature than the melting tank, and a molten product melted in the melting tank is pyrolyzed to produce a vapor-like product. A low-boiling-point hydrocarbon oil producing apparatus provided with a pyrolysis tank to be heated, a screw feeder for supplying raw material plastic to the melting tank at a normal temperature, and a heating means for heating the heat medium,
A supply system that guides the melt in the melting tank to the pyrolysis tank, a melting tank circulation system that branches from the supply system to the melting tank, and circulates and returns the melt in the melting tank, and a melt in the pyrolysis tank A reflux system that refluxes a part of the melt into the melting tank, a pyrolysis tank circulation system that branches from the reflux system to the pyrolysis tank, and circulates and returns the melt in the pyrolysis tank. Stirring means for stirring and mixing the raw material plastic, a wet neutralization device for introducing gas in the melting tank to neutralize and embed hydrogen chloride gas generated in the melting tank, A dry neutralization device for introducing the product to neutralize and bury the hydrogen chloride gas contained in the vaporous product; and control means, wherein the control means controls the melting tank circulation system and the pyrolysis tank circulation. System and adjust the melt in the melting tank to remove the polyvinyl chloride mixed with the raw plastic. During the appropriate time when the hydrochloric acid reaction is almost completed, while circulating through the melting tank circulation system to the melting tank and holding it in the tank, the melt in the pyrolysis tank is circulated to the pyrolysis tank through the pyrolysis tank circulation system, and then The supply system and the reflux system are preliminarily adjusted to guide the melt in the melting tank held for the appropriate time to the pyrolysis tank by the supply system, and a part of the melt in the pyrolysis tank is recycled to the reflux system. To the melting tank, and melt the appropriate volume of molten material in the melting tank.
Low boiling hydrocarbon oil, characterized in that pooled, and configured to hold said heating means to a suitable temperature to promote Tekisen adjusted to dehydrochlorination reaction temperature of polyvinyl chloride melt melting tank Manufacturing equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17934794A JP2988508B2 (en) | 1994-08-01 | 1994-08-01 | Method and apparatus for producing low-boiling hydrocarbon oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17934794A JP2988508B2 (en) | 1994-08-01 | 1994-08-01 | Method and apparatus for producing low-boiling hydrocarbon oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0841465A JPH0841465A (en) | 1996-02-13 |
| JP2988508B2 true JP2988508B2 (en) | 1999-12-13 |
Family
ID=16064260
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP17934794A Expired - Fee Related JP2988508B2 (en) | 1994-08-01 | 1994-08-01 | Method and apparatus for producing low-boiling hydrocarbon oil |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2988508B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3489407B2 (en) * | 1997-09-11 | 2004-01-19 | 株式会社日立製作所 | How to convert waste plastic to oil |
| WO2009054282A1 (en) * | 2007-10-23 | 2009-04-30 | Sunfuu Co., Ltd. | Oil recovery/reduction apparatus and method for oil recovery/reduction |
| EP2609146B1 (en) * | 2010-08-26 | 2015-04-15 | AHD Vagyonkezelö és Tanácsadó Kft. | Process for termical degradation of pvc and other wastes containing halogen-containing polymer waste |
| US20220389327A1 (en) * | 2019-11-14 | 2022-12-08 | Exxonmobil Chemical Patents Inc. | Process for feeding plastic waste material to a thermochemical or pyrolysis reactor |
-
1994
- 1994-08-01 JP JP17934794A patent/JP2988508B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0841465A (en) | 1996-02-13 |
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